Continuous process for scrubbing h2s from a gas stream and selectively producing elemental sulfur using four recycle water streams

ABSTRACT

H2S is removed from a gas stream and sulfur is selectively produced by the steps of: (1) sequentially scrubbing the gas with a first recycle water stream containing NH4OH and then with a second recycle water stream which is substantially NH4OH-free to produce a treated gas stream, which is reduced in H2S content and is substantially free of NH3, and a rich absorbent stream containing NH4HS; (2) catalytically reacting a portion of the rich absorbent stream and a third recycle water stream containing NH4HS and NH4OH with a first air stream to produce a liquid stream containing ammonium polysulfide and a gas stream containing NH3, H2S, H2O and N2; (3) catalytically reacting the liquid stream from step (2) and a fourth recycle water stream containing ammonium polysulfide with a second air stream to form a substantially sulfide-free water stream containing NH4OH and (NH4)2S2O3, a gas stream containing NH3, H2O and N2 and a liquid sulfur stream; (4) recovering a portion of the water stream from step (3) as at least a portion of the first recycle water stream and passing same to step (1); (5) stripping NH3 from another portion of the water stream formed in step (3) to make a sulfideand ammonia-free water stream containing (NH4)2S2O3; (6) passing a portion of the water stream from step (5) to step (1) as the second recycle water stream; (7) reacting another portion of the water stream from step (5) and another portion of the rich absorbent stream to form the fourth recycle water stream and passing same to step (3); and (8) scrubbing NH3 and H2S from the gas streams produced in steps (2) and (3) to form the third recycle water stream and passing same to step (2).

United State S Patent 1 Hamblin [54] CONTINUOUS PROCESS FOR SCRUBBING H28 FROM A GAS STREAM AND SELECTIVELY PRODUCING ELEMENTAL SULFUR USING FOUR RECYCLE WATER STREAMS [76] Inventor: Robert J. J. Hamblin, Des Plaines,

I73] Assignee: Universal Oil Products Company,

Des Plaines, Ill.

[22] Filed: July 30, 1971 [21] Appl. No.: 167,735

Related U.S. Application Data [63] Continuation-impart of Ser. No. 773,211, Nov. 4,

1968, Pat. NO. 3,627,465.

Primary Examiner-Oscar R. Vertiz Assistant ExaminerGeorge O. Peters Attorney-James R. Hoatson, Jr. et al.

111 3,715,426 1 Feb. 6, 1973 7 1 ABSTRACT H S is removed from a gas stream and sulfur is selectively produced by the steps of: (l) sequentially scrubbing the gas with a first recycle water stream containing NH OH and then with a second recycle water stream which is substantially NH Ol-l-free to produce a treated gas stream, which is reduced in H S content and is substantially free of NH and a rich absorbent stream containing NH HS; (2) catalytically reacting a portion of the rich absorbent stream and a third recycle water stream containing NH HS and NH OH with a first air stream to produce a liquid stream containing ammonium polysulfide and a gas stream containing NH H 8, H 0 and N (3) catalytically reacting the liquid stream from step (2) and a fourth recycle water stream containing ammonium polysulfide with a second air stream to form a substantially sulfide-free water stream containing NH OH and (NH SO a gas stream containing NH 8 H D and N 2 and a liquid sulfur stream; (4) recovering a portion of the water stream from step (3) as at least a portion of the first recycle water stream and passing same to step (1); (5) stripping Nl-l from another portion of the water stream formed in step (3) to make a sulfideand ammonia-free water stream containing (NI-10 8 0 (6) passing a portion of the water stream from step (5),to step l) as the second recycle water stream; (7)

' reacting another portion of the water stream from step (5) and another portion of the rich absorbent stream to form the fourth recycle water stream and passing same to step (3); and (8) scrubbing Nl-l and H 8 from the gas streams produced in steps (2) and (3) to form the third recycle water stream and passing same to step (2 18 Claims, 1 Drawing Figure CONTINUOUS PROCESS FOR SCRUBBING H25 FROM A GAS STREAM AND SELECTIVELY PRODUCING ELEMENTAL SULFUR USING FOUR RECYCLE WATER STREAMS CROSS-REFERENCES TO RELATED APPLICATIONS This application is a continuation-in-part of my prior,

copending application Ser. No. 773,211 which was filed on Nov. 4, 1968 now U.S. Pat. No. 3,627,465.

The subject of the present invention is a novel, continuous process for conveniently and economically removing H 8 from a gas stream, by sequentially scrubbing the gas stream with an ammoniacal absorbent stream and with an ammonia-free absorbent stream to form a sulfide-rich absorbent stream, without contaminating the treated gas stream with Nl-l and for recovering elemental sulfur from the resulting rich absorbent stream while continuously regenerating the two absorbent streams and selectively reducing thiosulfate by-product. More precisely, the present invention is based on my finding of a convenient and simple method for treating a water stream containing NH HS to produce elemental sulfur, control thiosulfate' byproduct and form two water streams: one containing NH OH and one substantially free of NH OH, coupled with my recognition that an H s-scrubbing step can be conveniently and simply interconnected with this treating method by means of these two water streams to enable the continuous and efficient scrubbing of a gas stream containing H 8 without contaminating the treated gas stream with substantial amounts of NH The removal of H 8 from a gas stream is a problem that has long confronted and challenged workers in many diverse industries. One example is in the natural gas industry where the H 8 content of certain gas streams recovered from natural gas deposits in many areas of the world is often too high for commercial acceptance. Another example is in the manufactured gas industry or the coke-making industry where coal gas containing unacceptable amounts of H 8 is commonly produced by the destructive distillation of bituminous coal having a high sulfur content. Yet another example is found in the manufacture of water gas or synthesis gas where it is not unusual to produce gas streams containing H 8 by passing steam over a bed of incandescent coke or coal containing a minor amount of sulfur.

More frequently, this problem is encountered in the petroleum refining industry because the principal raw material used, crude oil, typically contains a minor amount of sulfur--principally in the form of organic sulfur compounds. During the course of the many processes to which the crude oil or fractions thereof are subjected, one or more gas streams containing H 5 are quite commonly produced. For example, in many cases one of the product streams from a hydrocarbon conversion process is a gas stream containing H 8 in admixture with hydrogen and/or with light normally gaseous hydrocarbonsmainly, C -C As is well known in the art, the presence of H 8 in these refinery gas streams can cause a number of detrimental problems in subsequent processing steps such as: corrosion of process equipment, deterioration and deactivation of catalysts, undesired side reactions, increases in process pressure requirements, increase in gas compressor capacity, etc.

Regardless of the source of the gas stream containing H 8, the problem of removing H 8 therefrom has been solved in a number of different ways which generally involve one or more of the following techniques: selective absorption with a wide variety of absorbents, adsorption by a suitable adsorbent, selective reaction with a reagent which produces an easily separable product, etc. The details of these techniques are well known to those skilled in the art. One old and well-known solu tion to this H 8 removal problem involves scrubbing the gas stream with an ammoniacal aqueous solution. For example, in Germany the Perox process, which uses ammonia scrubbing, has been widely used for coal gas purification. Despite the considerable amount of effort that has been devoted to developing an acceptable solution to this problem involving scrubbing with an ammoniacal solution, the use of ammoniacal scrubbing has not been universally accepted in the gas treating art as the preferred method for removing H 8 from a gas stream primarily because of a number of operational difficulties associated with its implementation. One difficulty involves the relatively high partial pressure of ammonia at preferred scrubbing temperatures which generally requires that the scrubbing step be conducted with a relatively dilute ammonia solution or under relatively high pressure. The use of a dilute scrubbing solution in turn quite commonly forces the addition of a separate water wash step after the ammonia scrubbing step in order to remove ammonia from the treated gas stream. in addition, the use of dilute scrubbing solutions typically increases substantially the regeneration costs where the regeneration step is conducted at a considerably higher temperature than the scrubbing step, although some of this heat load can be recovered by a suitable heat exchanging procedure. Another difficulty is associated with the regeneration of the rich absorbent solution withdrawn from the H S-scrubbing step. In order to minimize the requirements of the scrubbing step for water and ammonia, it is necessary to remove sulfide from this rich absorbent. Several regeneration procedures have been proposed but they typically have involved the use of absorbent-soluble catalysts such as hydroquinone and have had problems such as contamination of the sulfur product with the catalyst, excessive formation of undesired by-products such as ammonium sulfate and thiosulfate and loss of scrubbing solution and catalyst during the periodic purges that are generally required to remove side products from the system. Other difficulties have been associated with the recovery of the elemental sulfur from the regeneration step where in some processes it has been customary to form a froth of sulfur in the absorbent regeneration vessel which then must be skimmed off and filtered. In short, it is clear that there are a significant number of technical problems associated with the prior art methods for removing H 8 from a gas stream by the method of scrubbing with an ammoniacal solution.

As a result of my investigations of methods of treating water streams containing NH HS, I disclosed in my prior application a new approach to the use of ammonia scrubbing for the solution of this H S removal problem which approach overcomes many of the difficulties experienced in the prior art. The basic concept of my approach involves the continuous production in the regeneration section via a simple, economic procedure of two separate recycle water streams, one containing NI-I OH and one substantially free of NH OI-I and the interconnection of the H S-scrubbing step and the regeneration section by means of these two recycle streams in a manner that minimizes the amount of ammonia carried out of the system via the treated gas stream. In my prior application, I disclosed a solution to the problem of scrubbing an H S-containing stream with ammoniacal solution wherein the sour gas stream was scrubbed with the two separate recycle water streams, one containing NH OH and one substantially free of NI-I,,OH, to form a rich absorbent containing NI-I,I-IS. According to the disclosed solution, the rich absorbent solution was then continuously regenerated by contacting it with a solid catalyst in the presence of oxygen at oxidizing conditions resulting in the formation of a solution containing ammonium polysulfide followed by thermal decomposition of the ammonium polysulfide to form an elemental sulfur product and produce the two recycle water streams. I have now ascertained that: (l) the scrubbing process disclosed in my prior application can be substantially improved by selectively oxidizing the ammonium polysulfide solution to form liquid sulfur and a substantially sulfide-free water stream which then can be easily treated to yield the two recycle water streams necessary for the operation of the H s-scrubbing step, and (2) the amount of ammonium thiosulfate by-product formed in the process can be controlled by a selective reduction reaction. This approach increases the yield of sulfur and eliminates the step of thermally decomposing ammonium polysulfide with its attendant high utility requirements and necessity for rather large recycle of unreacted sulfide and substitutes a straightforward, selective catalytic oxidation of the ammonium polysulfide to elemental sulfur. These modifications of my prior process result in an improved process which has the following advantages: (1) the sulfur product is liquid and is not contaminated with detrimental salts; (2) the ammonia lost from the system in the treated gas stream is held to extremely low levels; (3) the scrubbing solution is not highly corrosive and metallurgy problems are minimized; (4) the catalyst utilized in the two oxidation steps are highly selective thereby minimizing undesired by-products; (5) only a minimum amount of water is evaporated in the regeneration section thereby holding heat loads to minimum levels; (6) the selectivity for elemental sulfur on a per pass basis, is quite high, approaching 95 percent yield of elemental sulfur, thereby minimizing sulfide recycle from the oxidation steps; (7) the requirements of the resulting process for water is minimized by the use of recycle water streams and by the fact that water is one of the products of the oxidation reactions in the regeneration section; (8) catalyst losses in the product sulfur stream are eliminated; and (9) ammonium thiosulfate byproduct production is controlled and sharply reduced, thereby increasing yield of sulfur on an overall basis.

It is, accordingly, a principal object of the present invention to provide improvements in a process for removing H S from a gas stream with an ammoniacal solution wherein the regeneration of the rich absorbent solution involves selective oxidation of sulfide to elemental sulfur. A second object is to provide a simple procedure for minimizing the amount of reboil heat which must be utilized in the regeneration section of such a process. Another object is to provide a simple technique for removing H 8 from a gas stream with an ammoniacal solution with subsequent regeneration of the rich absorbent stream to selectively yield elemental sulfur and a regenerated absorbent stream. Yet another object is to control and minimize thiosulfate byproduct of such a process. Still another object is to provide a process for scrubbing H S from a gas stream which is relatively simple, effective and economical because the absorbent utilized is continuously and efficiently regenerated.

In brief summary, the present invention is a continuous, closed-loop process for treating a gas stream containing H 8 and for producing elemental sulfur therefrom. In the first step of the process the input gas stream is introduced into the lower region of a first gas scrubbing zone which is typically a vertically positioned tower containing suitable gas-liquid contacting means. Also in this first step a first recycle water stream contacting NH OI-I is introduced into the middle region of this first scrubbing zone and a second recycle water stream which is substantially free of ammonia and sulfide is introduced into this scrubbing zone above the point of introduction of the first recycle water stream. According to the second step, this first scrubbing zone is maintained at countercurrent gas-liquid contacting conditions selected to produce a gaseous overhead stream which is substantially reduced in H 8 content and is substantially free of NI-I and an aqueous bottom stream, the rich absorbent stream containing NH I-IS and in most cases NH OH. In the next step, a mixture of a first portion of the aqueous bottom stream from this first scrubbing zone, a first air stream and a third recycle water stream containing (NH,) S O;,, NH OI-I and NHJ-IS is reacted, in a first oxidation zone, with a solid catalyst at oxidation conditions selected to form an effluent stream containing ammonium polysulfide (NH SD NI-I DH, H 9 and N and in many cases unreacted NHJ-IS. The effluent stream from this first oxidation step is then separated, in a first conventional gas-liquid separating zone, into a gas stream containing N H 0, H 8 and NH;, and a liquid stream containing ammonium polysulfide, NH OH, H 0 and (NH ),S O In the second oxidation step, the liquid stream from the first gas-liquid separating zone, a fourth recycle water stream containing ammonium polysulfide and unreacted (NH S O and a second air stream are reacted with a solid catalyst at oxidizing conditions, including a temperature greater than or equal to the melting point of sulfur and a pressure sufficient to maintain this liquid stream in the liquid state, selected to form a liquid sulfur stream and an effluent stream containing (NI-M 8 0 NH,OI-I, H 0 and N After this second oxidation step, the effluent stream therefrom is separated, in a second gas-liquid separating zone, into a gas stream containing N H 0 and NH;, and a substantially sulfide-free water stream containing (NI-I0 8!) and NH DH. According to the next step of the process, a first portion of the water stream formed in the second gas-liquid separating zone is subjected to conditions designed to strip NH: and produce an overhead vapor stream containing NH and H 0 and a bottom water stream which is substantially free of ammonia and sulfide and which contains a minor amount of (Nl-I S O A first portion of the bottom water stream from this ammonia stripping step is then reacted with a second portion of the aqueous bottom stream from the first scrubbing zone, in amounts such that the mole ratio of sulfide to thiosulfate reacted is not greater than 2:1, at thiosulfate reduction conditions effective to form an effluent stream containing ammonium polysulfide and unreacted (NH,) S O A second portion of this bottom water stream from the ammoniastripping step is then charged to a second gas-liquid scrubbing zone wherein it is utilized to scrub H 8 and NI-I from the gas streams produced in the first and second gas-liquid separating zones. Thereafter, the ammonia and sulfide rich bottom stream from this second scrubbing zone is charged to the first oxidation zone as the third recycle water stream. The second recycle water stream is then recovered as a third portion of the bottom water stream withdrawn from the ammoniastripping step and passed to the first scrubbing zone. Similarly, the fourth recycle water stream is obtained from the effluent stream from the reduction step and passed to the second oxidation step. Lastly, the first recycle water stream is prepared by condensing at least a portion of the overhead vapor stream from the ammonia-stripping step to form an ammoniacal water stream which is then combined with a second portion of the water stream withdrawn from the second gasliquid separating zone and the resulting water stream is passed to the first scrubbing zone.

Other embodiments and objects of the present invention encompass details about particular input streams, output streams, and the mechanics associated with each of the essential and preferred steps thereof. These are hereinafter disclosed in the following detailed discussion of the present invention.

The invention will be further described with reference to the attached drawing which is a schematic outline of the process under discussion. The attached drawing is merely intended as a general representation of a preferred flow scheme with no intent to give details about vessels, heaters, condensers, pumps, compressors, valves, process control equipment, etc., except where a knowledge of these devices is essential to the understanding of the present invention or would not be self-evident to one skilled in the gas treating art.

Referring now to the attached drawing, a gas stream containing H S enters the process through line 1 and is charged to the lower region of the first scrubbing zone, zone 2. The gas stream may be derived from a number of different sources and may be a coal gas, an oil gas, a water gas, a natural gas, a refinery gas and the like gas streams. In order to avoid confusion, some of the various types of gas streams which can be charged to this process are defined'as follows: (1) coal gas is a mixture of gases produced by the destructive distillation of coal; (2) an oil gas is a gas derived from petroleum by the interaction of oil vapors and steam at high temperatures;

' (3) a water gas, or a synthesis gas as it is sometimes called, is a gas made by decomposing steam by passing it over a bed of incandescent coke or coal, and in some cases it is made by the high temperature reduction of steam with natural gases or similar hydrocarbons; (4) a natural gas is a mixture of low molecular weight paraffin hydrocarbons--typically C -C and, (5) a refinery gas is a mixture of low molecular weight hydrocarbons and/or hydrogen gases produced in converting and distilling hydrocarbons. In all cases, the gas stream to be treated by the present invention will contain H 8 in an amount ranging from about 0.01 mole percent up to 5 about 50 mole percent or more. Typically, the amount of H 8 contained in this gas stream will be about 1 to about mole percent. In addition, in some cases, the gas stream may contain ammonia, and in this case the present invention will also substantially remove and recover the ammonia from the gas stream.

Zone 2 is preferably a vertically positioned tower containing suitable means for achieving intimate contact between a gas stream and a liquid stream. Suitable contracting means are trays, plates, baffles or any other suitable packing material such as Raschig rings known to those skilled in the art. Zone 2 is conveniently divided into three regions: a bottom region where the input gas stream enters; a middle region where a first recycle water stream enters, and a top region where a second recycle water stream is injected. The input gas stream is charged via line 1 to the bottom region of zone 2 where it intimately contacts a descending water stream which is a mixture of the first recycle water stream, which is injected via line 16, and a second recycle water stream, which enters zone 2 by means of line 23. As indicated hereinbefore, it is an essential feature of the present invention that the first recycle water stream contains NI-I OH and that the second recycle water stream is substantially free of NH OI-I. The amount of NH.,Oh contained in the first recycle water stream may range from about 1 wt. up to about 50 wt. or more. In general, it is necessary to inject sufficient NI-I into zone 2 via line 16 to provide at least one mole of NH per mole of H 8 entering zone 2 via line 1, and, more preferably, about 1 to about 5 or more moles of NH; per mole of H 8. Accordingly, for a particular H 8 loading on zone 2, the NI-I OI-I concentration and operating conditions are selected to provide an Nl-l lfl s mole ratio within the specified range and to reduce the H 5 content of treated gas stream to the desired low level which typically is of the order of 10 to 500 vol. ppm. of the exit gas stream leaving zone 2 by means ofline 3.

In the upper region of zone 2 the partially scrubbed gas stream is countercurrently contacted with the second recycle water stream under conditions designed to remove substantially all volatilized NI-I from the gas stream. This second recycle water stream is substantially free of NH typically less than 300 wt. ppm.- because it is a portion of the bottom water stream from ammonia stripping zone 18 as is explained hereinafter. The rate of circulation of this second recycle water stream is generally conveniently selected for a particular gas input stream and NH /H S loading on the basis of a simple experiment designed to determine the good results are obtained at a temperature of 50F. to about 150F. and a pressure ranging from about 1 to about 500 atmospheres. For example, excellent results are obtained at a temperature of about 70F. and a pressure of about atmospheres.

Following contact of the gas stream with the two recycle water streams, a treated gas stream is withdrawn from the upper region of zone 2 by means of line 3 and vented from the system. Similarly, an aqueous bottom stream containing Nl-LHS and typically some unreacted NH OH is withdrawn from the bottom region thereof via line 4. Although it is not essential, in a case where very dilute gas streams are being treated in zone 2, the bottom stream therefrom may be advantageously further treated to concentrate the NH HS contained therein to yield a water stream containing about 3 to wt. sulfur as Nl-LHS. Generally, this concentration step can be easily effected by stripping M1,, and H 8 from the bottom stream and redissolving the resulting gas stream in the required quantity of water or by recirculating at least a portion of this bottom stream around the lower region of zone 2. However, in most cases the amount of Nl-LHS contained in this bottom stream is sufficient to allow the direct passage of a portion of it to first oxidation zone 6 as is shown in the drawing. This is especially true when the amount of unreacted sulfide recycled to zone 6 via line 27 is sufficient to increase the concentration of sulfide in the combined water stream charged to zone 6 to about 3 to 15 wt. thereof.

Accordingly, in the embodiment disclosed in the drawing, the aqueous bottom stream from zone 2 is passed via line 4 to the junction of line 5 with line 4 where a first portion of it is passed to zone 6 via line 5. This first portion is commingled with a first air stream at the junction of line 32 with line 5 and the resulting mixture is then combined with a third recycle water stream at the junction of line 5 with line 27. This mixture of the three streams is then passed to first oxidation zone 6. The amount of oxygen contained in this first air stream is selected so that ammonium polysulfide is formed within zone 6. in order to effect polysulfide formation in zone 6, the amount of oxygen injected into this zone must be carefully regulated so that oxygen is reacted therein in an amount less than the stoichiometric amount required to oxidize all of the ammonium hydrosulfide salt charged to this zone to elemental sulfur. Since the stoichiometric amount of oxygen is 0.5 moles of oxygen per mole of sulfide, it is essential that the amount of oxygen charged to the treatment zone is sufficient to react less than 0.5 moles of 0 per mole of sulfide, and, preferably, about 0.25 to about 0.45 moles of oxygen per mole of sulfide salt. It is especially preferred to operate with an amount of oxygen sufficient to react about 0.4 moles of oxygen per mole of sulfide charged to this zone. Accordingly, the amount of oxygen, charged to zone 6 via lines 31 and 32, is selected such that sufficient unreacted sulfide remains available to form a water-soluble ammonium polysulfide with the elemental sulfur which is the product of the primary oxidation reaction. Since 1 mole of sulfide will react with many atoms of sulfur (for ammonium polysulfide it is typically about four atoms of sulfur per mole of sulfide), it is generally only neces- I sary that a small amount of sulfide remain unoxidized.

According to the present invention, a first portion of the aqueous bottom stream from zone 2 is passed to zone 6 wherein it is catalytically treated with oxygen at oxidizing conditions selected to produce an effluent stream containing ammonium polysulfide, Nl-LOH, (Ni- 9 3 H D, N ,and typically some unreacted NHJ-IS. A feature of the present invention is the commingling of the water stream feed to zone 6 with a third recycle water stream containing unreacted sulfide recovered from the effluent stream from reaction zone 6. This third recycle water stream may be commingled with the first portion of the aqueous bottom stream from zone 2 prior to its being passed into the first oxidation zone as is shown in the drawing; on the other hand, this recycle water stream can be injected into the oxidation zone at a plurality of injection points spaced along the direction of flow of the bottom stream through the first oxidation zone. The principal advantage of this latter procedure is that the recycle water stream acts as a quench stream for the exothermic reactions taking place within the first oxidation zone. Another advantage associated with use of the third recycle water stream is that the concentration of NH HS charged to the first oxidation zone is increased. Since it has been determined that the selectivity of the oxidation reaction occurring in zone 6 for elemental sulfur increases with the concentration of sulfide charged to this first oxidation step, the presence of sulfide in the recycle stream can be used to increase the selectivity for sulfur in zone 6. In fact, it is a preferred procedure to use the third recycle water stream to maintain the concentration of ammonium hydrosulfide in the combined water stream charged to zone 6 at about 3 to about 15 wt. calculated as elemental sulfur.

The oxidation catalysts utilized in first oxidation zone 6 and in subsequently described second oxidation zone 11 can be any suitable solid catalyst that is capable of accelerating the oxidation of ammonium hydrosulfide to elemental sulfur. Two particularly preferred classes of catalyst for these two oxidation steps are metallic sulfides, particularly iron group metallic sulfides, and metal phthalocyanines. It is to be recognized that it is not necessary to use the same type of catalyst in zones 6 and 11; however, operations are often simplified if the same type of catalyst is utilized.

The preferred metallic sulfide catalyst is selected from the iron group sulfides; that is the sulfides of nickel, cobalt, and iron, with nickel sulfide being especially preferred. Although it is possible to perform this oxidation step with a slurry of metallic sulfide particles, it is preferred that the metallic sulfide be combined with a suitable carrier material. Examples of suitable carrier materials are: charcoals, such as wood charcoal, bone charcoal, etc., which charcoals may or may not be activated prior to use; refractory inorganic oxides such as alumina, silica, zirconia, bauxite, etc.; activated carbons such as those commercially available under trade names of Norit, Nuchar, and Darco and other similar carbon materials familiar to those skilled in the art. in addition, other natural or synthetic highly porous inorganic carrier materials such as various forms of clay, kieselguhr, etc., may be used if desired. The preferred carrier materials for the metallic sulfide catalyst are alumina, particularly alpha-, gamma-, and eta-alumina,

and activated charcoal. Thus, nickel sulfide combined with alumina or nickel sulfide combined with activated carbon are particularly preferred catalysts for the oxidation step. In general, the metallic sulfide is preferably combined with the carrier material in an amount which is catalytically effective; typically good results are obtained with an amount sufficient to result in a final composite containing about 0.l to about 30 or more wt. of the metallic component, calculated as the elemental metal. For the preferred nickel sulfide catalyst, excellent results are obtained with about i to about l wt. nickel as nickel sulfide on an activated carbon support or on an alumina support.

An especially preferred catalyst for use in the oxidation steps of the present invention is a metal phthalocyanine compound combined with a suitable carrier material. Particularly preferred metal phthalocyanine compounds include those of cobalt and vanadium. Other metal phthalocyanine compounds that may be used include those of iron, nickel, copper, molybdenum, manganese, tungsten, and the like. Moreover,

any suitable derivative of the metal phthalocyanine may be employed including the sulfonated derivatives and the carboxylated derivatives.,Any of the carrier materials previously mentioned in connection with the metallic sulfide catalysts can be utilized with the phthalocyanine compound; however, the preferred can rier material is activated carbon. Hence, a particularly preferred catalyst for use in the oxidation step comprises a cobalt or vanadium phthalocyanine sulfonate combined with an activated carbon carrier material. Additional details as to alternative carrier materials, methods of preparation, and the preferred amounts of catalytic components are given in the teachings of U. S. Pat. No. 3,108,081 for these phthalocyanine catalysts.

Although operation of zone 6 can be performed according to any of the methods taught in the art for simultanteously contacting a liquid stream and a gas stream with a solid catalyst, the preferred procedure involves a fixed bed of the solid catalyst disposed in the oxidation zone. The first portion of the aqueous bottom stream from zone 2 is then passed therethrough in either upward, radial, or downward flow and the first air stream is charged in either concurrent or countercurrent flow relative to the water stream. The preferred procedure is to operate downflow with both streams being charged in concurrent fashion. Because one of the products of this oxidation step is elemental sulfur, there is a substantial catalyst contamination problem caused by the deposition of this elemental sulfur on the fixed 3 bed of the catalyst. In order to avoid sulfur deposition on the catalyst, it is necessary to operate so that the net sulfur made in this zone is reacted with excess sulfide to form a water-soluble ammonium polysulfide.

' Regarding the conditions utilized in first oxidation zone 6, it is preferred to utilize a temperature in the range of about 75 to about 200F., with a temperature of about 100 to about 175F. yielding best results. The sulfide oxidation reaction is not too sensitive to pressure; and, accordingly, any pressure which maintains the water stream charged to zone 6 substantially in the liquid phase maybe utilized. In general, it is preferred to operate at the lowest possible pressure which is sufficient to maintain the elemental sulfur in combination as the water-soluble ammonium polysulfide, and although pressures of about 1 to about 30 psig. may be used, a pressure of about 1 to about 20 psig. is particularly preferred. Additionally, it is preferred to operate on the basis of a combined stream liquid hourly space velocity which is defined as the volume charge rate per hour of the first position of the aqueous bottom stream from zone 2 plus the third recycle water stream divided by a total volume of the catalyst bed in zone 6. This parameter is preferably selected from the range of about 0.1 to about 20 hr. with a value of about 1 to 10 hr. giving best results.

An effluent stream is then withdrawn from zone 6 via line 7 and found to contain ammonium polysulfide, NH,OH, (NH S O H O, N in many cases unreacted Nl-LHS and typically some unreacted 0 This stream is passed via line 7 to first gas-liquid separating zone 8 and therein separated into a gas stream, withdrawn via line 9, containing N H 0, H 8, Nll and typically some unreacted O and a liquid stream, withdrawn via line 10, containing ammonium polysulfide, NH Ol-l, (NH S O H 0 and typically some unreacted NH HS. This first separation step is preferably performed at about the temperature and pressure maintained at the outlet from the first oxidation step. It is to be noted that this first separation step can be perfon'ned in the lower region of first oxidation zone 6 if desired by use of a suitable baffling arrangement.

The liquid stream from first separation zone 8 is then passed via line 10 to the junction of line 31 with line 10 wherein it is commingled with a second air stream which enters the system via line 31 and to the junction of line 10 with line 30 where it is commingled with a fourth recycle water stream. The resulting mixture of air and liquid is then heated to the desired conversion temperature by heating means (not shown) and passed into second oxidation zone 11. As 'perviously explained, zone 11 contains a fixed bed of a solid oxidation catalyst of the type already characterized.

The function of second oxidation zone 11 is to selectively oxidize the ammonium polysulfide charged thereto to liquid sulfur while minimizing the formation of undesired by-products-primarily (Ni-[0 8 0 Second oxidation zone 11 is operated at conditions designed to accomplish this function. They are in general relatively more severe than those utilized in the first reaction zone, and typically include: (1) a temperature greater than or equal to the melting point of sulfur-that is, a temperature of at least 235F. and more typically about 235 to about 325F., with best results obtained at a temperature of about 235 to about 265F; (2) a pressure sufficient to maintain at least a portion of the liquid stream from the first separatingzone in the liquid phase-although any pressure meeting this requirement can be used, it is distinctly preferred to utilize a pressure which is quite close to the minimum pressure required to maintain a liquid phase at the temperature selected; thus an especially. preferred pressure is one that is'about l to about 1.5 times this minimum pressure; (3) a combined stream liquid hourly space velocity selected from the range of about 0.5 to about 10 hr. For example, ex-

cellent results have been obtained when this secondv reaction zone is operated at a temperature of about 235 to 265 F., a reactor pressure of about 20 to 40 psig. and a liquid hourly space velocity of about i to hr. Zone 11 is preferably operated in a manner similar to zone 6.

The amount of oxygen charged to zone 11 by means of the second air stream is preferably an amount less than that utilized in the first reaction zone. Typically, the amount of oxygen reacted in this second oxidation step is not greater than 2 times the stoichiometric amount required to completely oxidize all the sulfide contained in the liquid stream charged thereto to sulfur; in fact, best results are ordinarily obtained at an oxygen to sulfide mole ratio corresponding to about 0.5:1 to about 0.9: 1.

After the desired reaction between oxygen and ammonium polysulfide is accomplished in zone 11, an effluent stream containing (NH,),S O NH Ol-l, H O, N and possibly a minor amount of unreacted O is withdrawn therefrom and passed via line 13 to second separating zone 14. It is to be noted that a feature of the operation of zone 11 is that the effluent stream withdrawn therefrom will be substantially free of sulfide; this is primarily caused by the high temperature utilized therein which greatly accelerates the oxidation of sulfide. In fact, the principal by-product of the reaction occurring in zone 11 is (Nl-lo S O ltis typically formed therein in an amount corresponding to about to 40 percent of the sulfide charged to zone 1 1.

Also withdrawn from zone 11 via line 12 is a liquid sulfur stream which is the principal product stream of the present process. Since zone 11 is operated at conditions which insure that any sulfur formed therein is liquid and since liquid sulfur is readily separable from the rest of the products of the reaction occurring in zone 11, it is generally a preferred practice to allow a liquid sulfur phase to separate from a water phase in the bottom of zone 11, although the sulfur separation can be performed in a separate separating zone such as zone 14 if desired. This sulfur stream is not contaminated with any salts, catalysts or other undesirable ingredients and is essentially 99 percent pure bright sulfur.

Second separating zone 14 is operated in a manner similar to the first separating zone to form a gas stream, withdrawn via line 15, containing N,, [1,0 and NH and a substantially sulfide-free water stream, withdrawn via line 16, containing (NH,),S;O, and NH OH. Once again this separation can be allowed to occur within the bottom region of zone 11 by using suitable baffling means if desired. In this latter case zone 14 would then of course be the lower region of zone 11. In some cases, the effluent stream from zone 11 can be cooled by suitable means (not shown) to a temperature of about 25 to about 200F. before being sent to separating zone 14. Zone 14 is typically operated at a pressure which approximates that used in zone 11.

The substantially sulfide-free water stream formed in zone 14 is withdrawn therefrom via line 16 and split into two portions at the junction ofline 17 with line 16. The first portion of this stream continues on via line 17 to the lower region of stripping zone 18. The second portion of this water stream is recirculated to first scrubbing zone 2 via line 16 as the first recycle water stream after it is combined with a portion of the ammoniacal water stream formed in subsequently described zone 18.

The function of stripping zone 18 is to strip NH, from the first portion of the water stream coming from the second separating zone. Since ammonia is a relatively volatile substance, this stripping operation is rather easily accomplished. Obviously, the temperature utilized should be relatively high and the pressure relatively low; specific stripping conditions are well known to those skilled in the art. Suitable heating means, such as a reboiler, a steam coil or the like, can be utilized to maintain the bottom of zone 18 at the desired stripping temperature. The stripping gas utilized can be generated in situ by heating means designed to generate upflowing water vapors or can be supplied from an external source. Regardless of how zone 18 is operated, an overhead vapor stream, withdrawn via line 20, containing NH, and H 0 will be produced therein in an amount sufficient to take substantially all the entering ammonia overhead. The bottom water stream, withdrawn from zone 18 via line 19, will consequently contain a minor amount (NI-1.0 8 0 but otherwise be substantially free of ammonia and sulfide.

At least a portion of the overhead vapor stream from zone 18 is preferably condensed (by means not shown) to form an ammoniacal water stream, a part of which can be recirculated to stripping zone 18 as reflux via line 22 and another part of which is passed via line 20 and 21 to the junction of line 21 with line 16 whereat it is combined with a second portion of the water stream from zone 14 in order to form the first recycle water stream. The return of this ammonia stream to admixture with the second portion of the water stream from zone 14 is necessary in order to maintain the proper amount of Nl-LOH in the regenerated first absorbent stream because the amount of NH; taken overhead in zone 18 is determined not by NH product requirements (if any) but on the need for an ammonia-free water stream for use in zones 2 and 25. Of course, if NH is present in the gas stream treated in zone 2 then a portion of the overhead vapor stream produced in zone 18 is withdrawn from the system via line 20 as an ammonia product stream. In general, it is preferred to withdraw the ammonia product stream after a portion of same is condensed because this procedure acts to enrich the ammonia product stream withdrawn from the system by means of line 20. Of course, where NH, is not present in the input gas stream entering the system via line 1 then line 20 is blocked off and makeup NH or NH,OH must be continuously added to the system via line 33 in order to make up for that lost from the system in the form of the very minor amount of (NH SO 3 by-product and the inevitable small losses in the vent gas streams.

A first portion of the'bottom water stream from NH:,- stripping zone 18 is withdrawn therefrom via lines 19 and 28, heated to the temperature used in zone 29 by suitable heating means (not shown) and passed to reduction zone 29 by means of line 28. The function of zone 29 is to reduce (NH,),S,O to ammonium polysulfide by a selective reaction which uses Nl-LHS as the reducing agent. In the case illustrated in the drawing the reducing agent is obtained by passing a second por tion of the bottom water stream from first scrubbing zone 2 to zone 29 by means of lines 4 and 28. This stream is also heated to the temperature used in zone 29 by conventional heating means (not shown). It is a feature of the present process that the amount of sulfide reactant passed to zone 29 is insufficient to react with all of the (NII S O, entering zone 29 to form ammonium polysulfide. The principal advantage of operating in this fashion is that the product stream from the reduction step can be passed directly to second oxidation zone 11. It is to be noted that both of the streams passed to zone 29 will contain (NH S O although the major portion comes from zone 18 via lines 19 and 28. Accordingly; zone 29 is operated so that the mole ratio of sulfide to thiosulfate reacted therein is not greaterthan 2: l with a value of about 1:1 to 2:1 being preferred. Because zone 29 is operated with a deficiency of sulfide reactant, the product streams therefrom will contain ammonium polysulfide and unreacted (NI-M 8 but only minor amounts of NI-I l-IS.

Reduction zone 29 is operated in any known manner for simultaneously contacting two 'liquid streams. Zone 29 may contain suitable contacting means for achieving intimate contact between the two liquid streams passed thereto. Since the reduction reaction performed in zone 29 is extremely fast at the reduction conditions hereinafter specified, the use of a catalyst in zone 29 is not necessary.

Zone 29 is operated at thiosulfate reduction conditions and these include: (1) a temperature of about 200 to about 700F., preferably about 325 to about 500F.; (2) a pressure which is sufficient to maintain liquid phase conditions in zone 29, generally a pressure of about 100 to about 5,000 psig.; and (3) a contact time of about 0.01 to about 2 hours.

The effluent stream withdrawn from zone 29 by means of line 30 contains ammonium polysulfide NI-I OI-I, unreacted (NI-I S O, and only a minor amount of NI-I HS. It is passed via lines 30 and to second oxidation zone 11 as the fourth recycle water stream. It is an excellent feed stream for second oxida' tion zone 16 because of its high polysulfide content and relatively low sulfide content.

It is to be noted that water is one of the products of the reactions occurring in zones 6, 11 and 29. Consequently, the net water product must be withdrawn from the system in some manner. If the input gas stream, entering the system via line 1, and/or the input air stream, entering via line 31, are not saturated with water than at least a portion of the water product will be withdrawn from the system via the vent gases in lines 3 and 26. In addition in the case where an NI-I product stream is withdrawn via line 20; an additional portion of the water product will exit via this route. In fact, in some cases the amount of water withdrawn from the system via these output streams may exceed the amount of water produced; in this case, makeup water will be added to the system via line 34; In the case where the amount of water removed from the system via the output streams in line 3, 26and 20 is not sufficient to remove the amount of water produced, a water stream containing a minor amount of the thiosulfate is withdrawn via line 19in order to prevent water accumulation in the system.

Returning now to the remaining portion of the bottom water stream from NH -stripping zone 18, it is passed via lines 19 and 23 to the junction of line 24 with line 23 where it is divided into a second and third portion. The second portion of this substantially ammoniaand sulfide-free water stream is then passed to the upper region of second scrubbing zone 25 via line 24. The third portion continues on via line 23 to the upper region of zone 2 as the second recycle water stream where it is used in the manner previously explained.

Turning now to the operation of the second scrubbing zone 25, it can be ascertained from the drawing that the gas streams produced in gas-liquid separating zones 8 and 14 are also charged thereto via lines 9 and 15 respectively. The scrubbing liquid for this zone is a second portion of the bottoms water stream from Nl-l -strip'ping zone 18 which enters zone 25 via line 2d as previously discussed. The function of zone 25 is to recapture the NH;, and H 8 present in the vent gas streams from the separating zones. Actually only NH is present in any substantial amount in the gas stream from zone 14 because of the essentially complete oxidation occurring in zone 11. Zone 25 may be operated in a number of different modes depending upon the economics of the particular application. In one mode of operation (shown in the drawing) both gas streams are combined at the junction of lines 9 and 15 and the resulting mixture passed into a single vertically positioned scrubbing vessel via line 9. In a second mode of operation of zone 25, two separate scrubbing vessels are provided with the scrubbing liquid being divided between them and the gas streams being separately treated in them. The principal advantage associated with this second mode is that the gas stream from zone 14 is available at a relatively higher pressure than that from zone 8 so that the separate scrubbing of the former stream can be conducted in a smaller vessel in a more efficient manner; however, this is counterbalanced by the additional capital investment required for the additional scrubbing vessel. In a third mode of operation of zone 25 two separate vessels are provided as in the second mode with the gas stream separately charged to them. However, all of the scrubbing liquid from line 24 is passed to one of the vessels with the bottom water stream from this vessel being used as the scrubbing fluid in the other vessel. Regardless of which mode of operation is utilized in zone 25, it preferably contains suitable contacting means for achieving intimate contact between the input gas and liquid streams. This zone is operated at countercurrent scrubbing conditions, typically including a relatively low temperature and relatively high pressure (if possible), and a liquid to gas loading (or circulation rate) sufficient to produce a vent gas stream which is substantially free of NH; and H 8. The vent gas stream is withdrawn from zone 25 via line 26 and vented-from the system. The aqueous bottom stream from zone 25 contains NH OI-I, (NI-I S O and NHJ-IS. It is withdrawn therefrom via line 27 and passed via lines 27 and 5 to the first oxidation zone as the third recycle water stream as pointed out supra. This third recycle water stream will contain substantially all of the NFL, and H 8 flashed off in separating zones 8 and 14.

During start-up of the process, the inventory of water containing NH OH is injected into the system via line 33. Likewise the inventory of ammoniaand sulfidefree water necessary for start-up is injected via line 34.

Typical results obtained with the present process are: (l) a conversion of sulfide in first oxidation zone 6 of about 60 to 90 percent at a selectivity for elemental sulfur (combined as polysulfide) of 80 to 95 percent; (2) a conversion of sulfide in second oxidation zone 11 of about 95 to 100 percent at a selectivity for sulfur of about 60 to 80 percent; and (3) on an overall basis, a conversion of about 90 to 95 percent or more of the sulfide present in the bottom water stream from zone 2 at a selectivity for elemental sulfur of about 90 to 98 percent thereof.

It is intended to cover, by the following claims, all changes and modifications of the above disclosure of the present invention which would be self-evident to a man of ordinary skill in the gas treating art.

I claim as my invention:

1. A continuous, closed-loop process for treating a gas stream containing H 8 and for producing elemental sulfur therefrom, said process comprising the steps of:

l. introducing said gas stream into the lower region of a first gas scrubbing zone, introducing a first recycle water stream containing NH OH into the middle region of the first scrubbing zone, and introducing a second recycle water stream which is substantially free of ammonia and sulfide into the first scrubbing zone at a point above the point of introduction of said first recycle stream;

2. maintaining said first scrubbing zone under countercurrent gas-liquid contact conditions selected to produce a gaseous overhead stream which is substantially reduced in H 8 content and is substantially free of NH and an aqueous bottom stream containing NH HS;

3. reacting a first portion of the aqueous bottom stream from step (2), a first air stream, a third recycle water stream containing NH HS, NH OH and (NH S O with a solid catalyst at oxidizing conditions selected to form an effluent stream containing ammonium polysulfide, (NI-M 8 NH OH, H 0 and N 4. separating the effluent stream from step (3) into a gas stream containing N H 0, H 8, and NH;, and a liquid stream containing ammonium polysulfide, NH OH, H 0, and (NH S O 5. reacting the liquid stream from step (4), a fourth recycle water stream containing ammonium polysulfide and unreacted (NH S O and a second air stream with a solid catalyst at oxidizing conditions, including a temperature greater than or equal to the melting point of sulfur and a pressure sufficient to maintain the liquid stream from step (4) in the liquid state, selected to form a liquid sulfur stream and an effluent stream containing (NH S O;,, NH OH, H 0 and N 6. separating the effluent stream from step (5) into a gas stream containing N H 0 and NH;, and a substantially sulfide-free water stream containing (NHJ SO ,and NH 0H;

7. stripping NH from a first portion of the water stream formed in step (6) to yield an overhead vapor stream containing NH and H 0 and a bottom water stream which is substantially free of ammonia and sulfide and which contains a minor amount of(NH S,O,;

8. reacting a first portion of the bottom water stream from step (7) with a second portion of the aqueous bottom stream from step (2), in amounts such that the mole ratio of sulfide to thiosulfate reacted is not greater than 2:1, at thiosulfate reduction conditions effective to form an effluent stream containing ammonium polysulfide and unreacted 02 5 9. passing the effluent stream from step (8) to step (5) as the fourth recycle water stream;

10. contacting a second portion of the bottom water stream from step (7) with the gas stream from step (4) and the gas stream from step (6), in a second scrubbing zone, at countercurrent gas-liquid contact conditions selected to form a nitrogen-rich overhead vent gas stream and an aqueous bottom stream containing NH OH, (NH S O and NH HS;

11. passing the aqueous bottom stream from step (10) to step (3) as the third recycle water stream;

12. passing a third portion of the bottom water stream from step (7) to step (I) as the second recycle water stream;

13. condensing at least a portion of the overhead vapor stream from step (7) to form an ammoniacal water stream; and,

14. combining at least a portion of the ammoniacal water stream formed in step (13) with a second portion of the water stream formed in step (6) to form the first recycle water stream and passing same to step l 2. A process as defined in claim 1 wherein the gas stream charged to step (1) contains H S and NH and wherein a portion of the overhead vapor stream from step (7) is withdrawn from the process as an ammoniacal product stream.

3. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise a phthalocyanine compound.

4. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise an iron group metallic sulfide combined with a carrier material.

5. A process as defined in claim 4 wherein the iron group metallic sulfide is nickel sulfide.

6. A process as defined in claim 1 wherein the amount of air charged to step (3) is sufficient to react about 0.4 moles of oxygen per mole of sulfide charged to said step.

7. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise cobalt phthalocyanine monosulfonate combined with an activated carbon or alumina carrier material.

8. A process as defined in claim 1 wherein the gas stream charged to step (I) is a coal gas containing H 8 and NH 9. A process as defined in claim 1 wherein the gas stream charged to step (1 is a water gas or a synthesis gas containing H 8.

10. A process as defined in claim 1 wherein the gas stream charged to step (1) is a natural gas containing H 8.

11. A process as defined in claim 1 wherein the gas stream charged to step (1) is a refinery gas containing H 8.

12. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (3) include a temperature of about 75 to about 200F. and a pressure of about 1 to about 30 psig.

13. A process as defined in claim 1 wherein the temperature utilized in step (5) is about 235 to about 325F.

14. A process as defined in claim 1 wherein the pressure utilized in step (5) is about 1 to bout 1.5 times the minimum pressure required to hold water in the liquid phase at the specific temperature utilized.

15. A process as defined in claim 1 wherein the pressure utilized in step (5) is just sufficient to maintain at least a portion of the liquid stream from step (4) in the liquid state.

16. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (3) include a temperature of about to about F. and a pressure of about i to about 20 psig.

17. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (5) include a temperature of about 235 to about 265F. and a pressure of about 20 to about 40 psig.

18. A process as defined in claim 1 wherein the thiosulfate reduction conditions utilized in step (8) include a temperature of about 200 to 700F., a pressure sufficient to maintain a liquid phase and a contact time of about 0.01 to 2 hours. 

1. A continuous, closed-loop process for treating a gas stream containing H2S and for producing elemental sulfur therefrom, said process comprising the steps of:
 1. introducing said gas stream into the lower region of a first gas scrubbing zone, introducing a first recycle water stream containing NH4OH into the middle region of the first scrubbing zone, and introducing a second recycle water stream which is substantially free of ammonia and sulfide into the first scrubbing zone at a point above the point of introduction of said first recycle stream;
 2. maintaining said first scrubbing zone under countercurrent gas-liquid contact conditions selected to produce a gaseous overhead stream which is substantially reduced in H2S content and is substantially free of NH3, and an aqueous bottom stream containing NH4HS;
 2. A process as defined in claim 1 wherein the gas stream charged to step (1) contains H2S and NH3 and wherein a portion of the overhead vapor stream from step (7) is withdrawn from the process as an ammoniacal product stream.
 3. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise a phthalocyanine compound.
 3. reacting a first portion of the aqueous bottom stream from step (2), a first air stream, a third recycle water stream containing NH4HS, NH4OH and (NH4)2S2O3 with a solid catalyst at oxidizing conditions selected to form an effluent stream containing ammonium polysulfide, (NH4)2S2O3, NH4OH, H2O and N2;
 4. separating the effluent stream from step (3) into a gas stream containing N2, H2O, H2S, and NH3, and a liquid stream containing ammonium polysulfide, NH4OH, H2O, and (NH4)2S2O3;
 4. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise an iron group metallic sulfide combined with a carrier material.
 5. A process as defined in claim 4 wherein the iron group metallic sulfide is nickel sulfide.
 5. reacting the liquid stream from step (4), a fourth recycle water stream containing ammonium polysulfide and unreacted (NH4)2S2O3, and a second air stream with a solid catalyst at oxidizing conditions, including a temperature greater than or equal to the melting point of sulfur and a pressure sufficient to maintain the liquid stream from step (4) in the liquid state, selected to form a liquid sulfur stream and an effluent stream containing (NH4)2S2O3, NH4OH, H2O and N2;
 6. separating the effluent stream from step (5) into a gas stream containing N2, H2O and NH3 and a substantially sulfide-free water stream containing (NH4)2S2O3 and NH4OH;
 6. A process as defined in claim 1 wherein the amount of air charged to step (3) is sufficient to react about 0.4 moles of oxygen per mole of sulfide charged to said step.
 7. A process as defined in claim 1 wherein the solid catalysts utilized in steps (3) and (5) comprise cobalt phthalocyanine monosulfonate combined with an activated carbon or alumina carrier material.
 7. stripping NH3 from a first portion of the water stream formed in step (6) to yield an overhead vapor stream containing NH3 and H2O and a bottom water stream which is substantially free of ammonia and sulfide and which contains a minor amount of (NH4)2S2O3;
 8. reacting a first portion of the bottom water stream from step (7) with a second portion of the aqueous bottom stream from step (2), in amounts such that the mole ratio of sulfide to thiosulfate reacted is not greater than 2:1, at thiosulfate reduction conditions effective to form an effluent stream containing ammonium polysulfide and unreacted (NH4)2S2O3;
 8. A process as defined in claim 1 wherein the gas stream charged to step (1) is a coal gas containing H2S and NH3.
 9. passing the effluent stream from step (8) to step (5) as the fourth recycle water stream;
 9. A process as defined in claim 1 wherein the gas stream charged to step (1) is a water gas or a synthesis gas containing H2S.
 10. A process as defined in claim 1 wherein the gas stream charged to step (1) is a natural gas containing H2S.
 10. contacting a second portion of the bottom water stream from step (7) with the gas stream from step (4) and the gas stream from step (6), in a second scrubbing zone, at countercurrent gas-liquid contact conditions selected to form a nitrogen-rich overhead vent gas stream and an aqueous bottom stream containing NH4OH, (NH4)2S2O3 and NH4HS;
 11. passing the aqueous bottom stream from step (10) to step (3) as the third recycle water stream;
 11. A process as defined in claim 1 wherein the gas stream charged to step (1) is a refinery gas containing H2S.
 12. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (3) include a temperature of about 75* to about 200*F. and a pressure of about 1 to about 30 psig.
 12. passing a third portion of the bottom water stream from step (7) to step (1) as the second recycle water stream;
 13. condensing at least a portion of the overhead vapor stream from step (7) to form an ammoniacal water stream; and,
 13. A process as defined in claim 1 wherein the temperature utilized in step (5) is about 235* to about 325*F.
 14. A process as defined in claim 1 wherein the pressure utilized in step (5) is about 1 to bout 1.5 times the minimum pressure required to hold water in the liquid phase at the specific temperature utilized.
 14. combining at least a portion of the ammoniacal water stream formed in step (13) with a second portion of the water stream formed in step (6) to form the first recycle water stream and passing same to step (1).
 15. A process as defined in claim 1 wherein the pressure utilized in step (5) is just sufficient to maintain at least a portion of the liquid stream from step (4) in the liquid state.
 16. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (3) include a temperature of about 100* to about 175*F. and a pressure of about 1 to about 20 psig.
 17. A process as defined in claim 1 wherein the oxidizing conditions utilized in step (5) include a temperature of about 235* to about 265*F. and a pressure of about 20 to about 40 psig. 